CN104807286B - Recycle the nitrogen gas liquefaction system of LNG cold energy - Google Patents
Recycle the nitrogen gas liquefaction system of LNG cold energy Download PDFInfo
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- CN104807286B CN104807286B CN201410616943.7A CN201410616943A CN104807286B CN 104807286 B CN104807286 B CN 104807286B CN 201410616943 A CN201410616943 A CN 201410616943A CN 104807286 B CN104807286 B CN 104807286B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 475
- 229910001873 dinitrogen Inorganic materials 0.000 title claims abstract description 26
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 228
- 239000007788 liquid Substances 0.000 claims abstract description 89
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 239000003345 natural gas Substances 0.000 claims abstract description 22
- 238000002309 gasification Methods 0.000 claims abstract description 14
- 238000003860 storage Methods 0.000 claims abstract description 12
- 238000004064 recycling Methods 0.000 claims abstract description 10
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 claims abstract description 8
- 230000006835 compression Effects 0.000 claims description 6
- 238000007906 compression Methods 0.000 claims description 6
- 238000003825 pressing Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 13
- 239000003949 liquefied natural gas Substances 0.000 description 69
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 54
- 238000000034 method Methods 0.000 description 39
- 229910052786 argon Inorganic materials 0.000 description 28
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 16
- 239000007789 gas Substances 0.000 description 13
- 239000000047 product Substances 0.000 description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 11
- 239000001301 oxygen Substances 0.000 description 11
- 229910052760 oxygen Inorganic materials 0.000 description 11
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 10
- 238000004519 manufacturing process Methods 0.000 description 8
- 238000005057 refrigeration Methods 0.000 description 8
- 238000001816 cooling Methods 0.000 description 6
- 125000004122 cyclic group Chemical group 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 238000005194 fractionation Methods 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 4
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 4
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
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- 239000000428 dust Substances 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- 238000003287 bathing Methods 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 2
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- 239000000284 extract Substances 0.000 description 2
- 229910052731 fluorine Inorganic materials 0.000 description 2
- 239000011737 fluorine Substances 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 230000002427 irreversible effect Effects 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000004378 air conditioning Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 230000002595 cold damage Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000002681 cryosurgery Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
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- 238000001914 filtration Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012299 nitrogen atmosphere Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0015—Nitrogen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
- F25J1/0224—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A kind of nitrogen gas liquefaction system recycling LNG cold energy that the present invention proposes, aim to provide a kind of structure simple, cold energy use rate is high, can reduce nitrogen compressor pressure rating and heat exchanger pressure rating, saves the nitrogen gas liquefaction system of energy consumption.The present invention can be achieved by following technical proposals: air separation column nitrogen overhead compresses through normal temperature compressed machine, in the nitrogen precooled heat exchanger of one-level, carry out heat exchange precooling with throttling re-heat low-pressure low-temperature natural gas, the low temperature nitrogen after precooling carry out with the middle LNG of pressure in cold heat exchanger in secondary nitrogen heat exchange obtain in cold nitrogen; In cold nitrogen absorb by three grades of nitrogen cryogenic liquefying heat exchangers the ultralow temperature cold energy liquefaction that throttlings gasification produces, the liquid nitrogen temperature of post liquefaction is down to-155 DEG C to-158 DEG C, most of low pressure liquid nitrogen that liquid nitrogen produces after choke valve throttling is as product introduction liquid nitrogen storage tank, small part low-pressure nitrogen, as circulating nitrogen gas, backflows after re-heat to nitrogen compressor entrance and recompresses in the nitrogen precooled heat exchanger of one-level.
Description
Technical field
The present invention relates to a kind of nitrogen gas liquefaction system recycling LNG cold energy, particularly relate to a kind of LNG cold energy recycle system making liquefaction of nitrogen.
Background technology
LNG (liquefied natural gas) not only contains huge cold, the more important thing is that its cold quality is very high.Along with the sustainable growth of LNG consumption, the cold that gasification produces also increases in succession.But traditional LNG gasification station adopts air-bathing gasifier that low temperature LNG (-160 DEG C) is heated to normal temperature and enters pipe network.In gasification, a large amount of cold energy is gathered in gasifier periphery and makes the air setting of periphery become water smoke thus cause cold pollution.
The cold energy discharged in LNG gasification can adopt direct or indirect method to be used.Direct Application way has cold energy generation, air liquefaction separation, cold storage warehouse, manufacture liquefied carbon dioxide, desalinization, air-conditioning and cold temperature culture cultivation etc.; Indirect utilization method has time point liquid oxygen obtained, liquid nitrogen to carry out cryogenic pulverization, sewage disposal, cryosurgery etc.
It is carry out degree of depth refrigerated separation to air that conventional air is separated project, needs a large amount of colds.The utilization of LNG cold energy the cold of LNG is passed to the medium needing cooling, reaches cold recoverable object.Compared with other LNG cold energy use method, in air separation unit, circulating nitrogen gas condensing temperature is lower, and between 145 ~ 235K, relatively little with the temperature difference of LNG, the irreversible loss in cold energy removal process is less, is more satisfactory and efficient Application way.
The air separation products be most widely used at present is oxygen, nitrogen, argon gas three kinds of gases.Oxygen is the active gas of reaction, is mainly used in metallurgy industry and chemical industry, can also be used for health care, municipal sewage treatment, metal solder and cutting, and because it has sufficient combustion-supporting property to any fuel, oxygen is also in burning process; Nitrogen can be widely used in industry and research field.In most application, nitrogen is cold-producing medium as a kind of physics or a kind of inert gas of chemistry; The most important chemical characteristic of argon gas is its inertia, and this characteristic becomes the protective gas of high-temperature process, is normally used in metallurgical and welding procedure.
The method that existing sky divides technology separation to go out the industrial gasses such as liquid oxygen, liquid nitrogen product is usually with the low-temperature liquefaction air separating method manufacture of Linde cycle or other improved loop.This method first air compressing to high pressure, make by the Air flow that compresses to normal temperature with cooling water, pressure-air throttling or expansion is allowed to produce low temperature, and the backflow of the Cryogenic air utilizing self to produce or isolated low temperature nitrogen and cryogenic oxygen is to cool pressure-air, so, pressure-air produces lower temperature by carrying out throttling at a lower temperature or expanding, and so circulate continuation, until make air liquefaction.After air liquefaction, utilize fractionating column to be separated according to heterogeneity boiling point difference in air, obtain oxygen, nitrogen, argon gas or their liquid that purity is very high.This method will be carried out under-150 DEG C ~-191 DEG C conditions, creates and tie up special low temperature and will consume a large amount of electric energy, and produce the cold energy loss of air separation.Utilize the document of the air separation unit of LNG cold energy little at present, the international RELATED APPLICATIONS through retrieval is also few.United States Patent (USP) solves the air-separating plant of LNG low-temperature receiver used, because of LNG demand fluctuation cause LNG cold under-supply time, adopt the liquid gasification of the inert gas of internal reservoir to supplement cold.A kind of elevated pressure nitrogen fluid of U.S. Patent Publication the cold quantity transmission of liquefied natural gas to cryogenic air separation plant, this invention relates to the process of the nitrogen liquefaction of producing with the associating cryogenic air separation plant improving refrigeration performance, the very low LNG of temperature is in gasification and transport simultaneously by as cold-producing medium, be characterized in being used as refrigerating medium with the nitrogen fluid of high pressure, air before LNG cold is passed to compression and nitrogen, elevated pressure nitrogen condenses is made again with the cold energy of LNG, produce by elevated pressure nitrogen the damp steam containing liquid nitrogen through throttling again in addition, go out liquid nitrogen through separation of produced.The disclosed one of Japan Patent: No:1090715 only uses high pressure fractionating column condensation segment and low pressure fractionating column without conventional high-pressure fractionating column, by the nitrogen recompression that low pressure fractionating column is produced, LNG is utilized to cool, fluorine Lyons is adopted to make the methods such as the refrigerating medium between low temperature LNG and compressed nitrogen and compressed air, raw air is only compressed to low pressure fractionating column operating pressure, produces liquid oxygen, liquid air and liquid argon.These methods propose the method utilizing LNG cold energy oxygen, nitrogen processed respectively from certain side.The weak point that current LNG cold energy produces the air-separating plant flow process of liquid oxygen and liquid nitrogen is: the oxygen liquefaction and the liquefaction of nitrogen that 1. consume a large amount of cold are temperature required lower than LNG gasification temperature-161 DEG C, must be supplemented by active refrigeration method.2. Compression alone air cooling can not balance the cold needed for liquid oxygen and liquid nitrogen, and energy consumption is very large.3. the LNG physical property of different component is different, and methane content is lower, and LNG gasification produces in cold temperature and moves, and available cold reduces, quality reduces.4. system will realize supplementing and balance of cold under different warm area.5. LNG cold energy use efficiency is on the low side.The parts of the air separation plant adopted in flow process are many, have: air cleaner, air compressor, aerial cooler, molecular screener adsorbing system, main heat exchanger, high pressure fractionating column, low pressure fractionating column, subcooler, argon gas fractionating system, liquid argon storage tank, liquid nitrogen storage tank, liquid oxygen storage tank, liquia air choke valve, liquid nitrogen choke valve, liquid ammonia switch valve, liquid oxygen switch valve, the blow through valve of Liquid Argon switch valve and connecting line and necessity, liquid air acetylene absorber, the useless nitrogen heater etc. of accessory system.Also set up with the nitrogen Inner eycle of LNG cold energy cooling and nitrogen outer circulation refrigeration system, and adopted fluorine Lyons of LNG cooling to be the refrigerating medium cooling pressure-air circulatory system.These newly-increased system flows run like this: air enters air compressor and is compressed to more than 0.5MPa after dust impurity is removed in air cleaner filtration, compressed air is cooled to 1 ~ 5 DEG C at aerial cooler by freon refrigerating medium, enter molecular screener adsorbing system, fall moisture content in air and the laggard pressure-air heat exchanger channels of becoming owner of heat exchange of carbon dioxide by molecular sieve adsorption; Main heat exchanger is heat-exchangers of the plate type, also be provided with the Medium pressure cycle nitrogen backheat passage of bottom in and top out and low-purity to give up channel of nitrogen, compressed air by the Medium pressure cycle nitrogen of about-180 DEG C that backflows and low-purity give up nitrogen cool, become saturated mode humid air, then enter high pressure fractionating column entrance; Air and liquid nitrogen condensation and the evaporation repeatedly on the column plate of multilayer from overhead streams in high pressure fractionating column, oxygen-enriched liquid air containing more liquid oxygen composition combines in the bottom of high pressure fractionating column, nitrogen combines in the top of high pressure fractionating column, and with low pressure fractionation column base liquid oxygen heat-shift after nitrogen be condensed into liquid.The liquid nitrogen that high pressure fractionating column top liquid nitrogen trap is collected is by exporting extraction, lower the temperature further through subcooler, about 0.14MPa is depressurized to again through liquid nitrogen choke valve, enter low pressure fractionating column top, as the phegma at low pressure fractionating column top, another part is banished liquid nitrogen storage tank and is stored after control valve.The oxygen-enriched liquid air of high pressure fractionation column base adsorbs to fall acetylene through liquid air acetylene absorber after outlet is flowed out, and cool through subcooler, again after the step-down of liquia air choke valve, enter the crude argon column of argon gas fractionating system, after oxygen-enriched liquid air is tentatively extracted argon gas in argon gas fractionating system, the pipeline of liquia air connected through low pressure fractionating column again connects and flows in low pressure fractionating column in the middle part of low pressure fractionating column, after the fractionation of low pressure fractionating column, high-purity liquid oxygen combines in low pressure fractionation column base, and to put to liquid oxygen storage tank through control valve from interface and store, the high pure nitrogen that low pressure fractionating column top is flowed out, after subcooler recovery section cold, enter the low pressure Inner eycle nitrogen backheat passage of low cycle of higher pressure nitrogen heat exchanger, cold is passed to the cycle of higher pressure nitrogen of the high pressure Inner eycle nitrogen heat release pipe of upper entering and lower leaving, heat up about to 110 ~ 120K, then enter medium pressure nitrogen air compressor to compress, be compressed to more than 1.0MPa, outlet temperature is more than after 220K, enter the sub-high pressure Inner eycle nitrogen heat release pipe of liquefied natural gas heat exchanger, release heat to LNG, temperature rolls back about 110 ~ 120K, enter high pressure nitrogen compressor compresses again to 5.0MPa, the high pressure Inner eycle nitrogen heat release pipe entering liquefied natural gas heat exchanger again releases heat to LNG, after temperature is down to about 110 ~ 120K, enter the high pressure Inner eycle nitrogen heat release pipe of low cycle of higher pressure nitrogen heat exchanger again, be cooled to about 100K further, and after be about 0.5MPa through Inner eycle nitrogen choke valve reducing pressure by regulating flow to high pressure fractionating column operating pressure, produce a large amount of liquid nitrogen and fractional saturation nitrogen, and after to enter the liquid nitrogen entrance of high pressure fractionating column through crossing.The Medium pressure cycle nitrogen that nitrogen outlet from high pressure fractionating column middle and upper part is drawn, just just starts the initial stage at device, through check valve, enters the Medium pressure cycle nitrogen backheat passage of main heat exchanger.When device normally runs, the nitrogen of outer circulation is no longer drawn from the nitrogen outlet of high pressure fractionating column middle and upper part, and draws the low temperature nitrogen after the throttling of nitrogen choke valve; The low temperature outer circulation nitrogen of about 90 ~ 100K passes to compressed air cold in the Medium pressure cycle nitrogen backheat passage of main heat exchanger, self backheat is to the temperature entering main heat exchanger entrance close to compressed air simultaneously, applicable flow is adjusted to through control valve, then enter the middle pressure outer circulation nitrogen heat releasing passage of liquefied natural gas heat exchanger, again the natural gas that is liquefied is cooled to about-120 DEG C, then enters outer circulation medium pressure nitrogen air compressor.Compressor is reduced to 3 ~ 5MPa nitrogen pressure, the temperature of circulating nitrogen gas is about 190K ~ 200K (-83 DEG C ~-73 DEG C), then enter the high pressure outer circulation nitrogen heat release pipe of liquefied natural gas heat exchanger, absorb LNG cold to be cooled to about 120K, to enter the high pressure outer circulation nitrogen heat release pipe of low-cycle of higher pressure nitrogen heat exchanger again, then be cooled to further and about close 100K.At the beginning of device starts, close choke valve, throttle opening, allows circulating air enter knockout tower, participates in fractionation.After being full of high pure nitrogen in circulation pipe, close choke valve, open outer circulation nitrogen choke valve and control valve, after throttling, pressure is also at about 0.5MPa.The low-purity nitrogen gas that low pressure fractionating column top is flowed out, with draw from high pressure fractionating column centre exit, converging through the nitrogen of the heat exchanger belonging to smart argon purifying column of argon gas fractionating system and the dirty little throttling N of nitrogen of argon liquid processed and heat exchanger, then after subcooler heat exchange, temperature enters the useless channel of nitrogen of main heat exchanger about 90K, absorb compressed-air actuated heat and by backheat at main heat exchanger, finally in exit by backheat to the temperature a little less than the porch compressed air several years.Backheat after useless nitrogen heater is heated by electric heater, delivers to molecular screener adsorbing system to the lower purified nitrogen gas of room temperature, and the moisture content in the molecular sieve tank removing desorption saturated steam in molecular sieve and carbon dioxide, make it regeneration, or by valve emptying.
The technological process utilizing LNG cold energy to carry out air separation has multiple, and external typical empty point flow process is that the air as raw material is entered air cleaner, enters air compressor after being removed by the dust in air.After compressor compression, pressure is that the air of 0.6MPa enters in air precooler and is precooled to 283K.Utilize the principle of pressure-variable adsorption the impurity such as carbon dioxide, moisture to be adsorbed in molecular sieve removing subsequently and freeze blocking to prevent subsequent pipeline.In cryogenic heat exchanger gaseous air by low-temperature circulating gaseous nitrogen atmosphere and low-purity discard to enter high pressure fractionating column after nitrogen is cooled to about 100K successively, low pressure fractionating column carries out each component of heat exchange gaseous air with low temperature liquid nitrogen wherein and liquefies successively.The liquid oxygen product of gained enters in liquid oxygen storage tank and stores, and liquid nitrogen product enters in liquid nitrogen storage tank and stores.Send in liquid argon storage tank store by argon purifier and the argon purifying column gained liquid argon product that carries out purifying and purify successively after using the deoxidation of hydrogen tank hydrogenation catalyst containing argon liquid gas.High pressure fractionating column flow out circulating gaseous nitrogen after cryogenic heat exchanger and raw air heat exchange, temperature rises to about 270K and enters main heat exchanger again and LNG heat-exchange temperature reduces to about 120K, then in cyclic nitrogen compressor, the high-pressure gaseous nitrogen of gained about 195K, about 2.5MPa is compressed, again enter main heat exchanger condensation temperature and reduce to about 120K, after nitrogen choke valve throttling decrease temperature and pressure to about 91K, 0.4MPa, enter after the liquid nitrogen entrance of high pressure fractionating column and air heat-exchange gasify and continue to circulate.The low-purity nitrogen gas of about the 100K that low pressure fractionating column top is flowed out, carries out cold energy recovery through cryogenic heat exchanger, after a part is heated by electric heater when needed, for the regeneration remainder emptying of air purifier Middle molecule sieve.The LNG of 110K, after main heat exchanger gasification, is warming up to about 250K, and shortage of heat part is undertaken supplementing adjustment or being supplemented by other cold energy retracting devices such as the air precoolers in system regulating by gas heater.
Prior art full-liquid air separation device adopts cryogenic rectification method, is utilize the difference of each component evaporating temperature in air they be separated and obtain fluid product, liquid oxygen, liquid nitrogen, liquid argon.Its full liquid space division flow process is made up of a series of continuous print process.Each process is an irreversible procedure, if any the cold process of race etc. of the heat exchange of the temperature difference, the resistant flow process of medium, expansion throttling process, air multicomponent cryogenic rectification, Cryo Equipment, capital produces exergy loss, namely exergy destruction, the summation of these exergy destruction realizes the merit required for these processes.The total exergy loss of this device is mainly lost by these units, wherein air compressor machine, cyclic nitrogen press, large percentage shared by the cold damage of high pressure heat exchanger.For full liquid space division flow process, energy consumption main in air separation unit is air compressor machine, cyclic nitrogen press, and decompressor, therefore needs a large amount of colds, and energy consumption is very high.The full liquid space division device of the two swell refrigeration flow process of traditional Medium pressure cycle, unit liquid energy consumption is about 1.0kWh/m3 (comprising liquid oxygen liquid nitrogen liquid argon).Specific works principle is, enters compressor, be compressed to 0.52MPa in air separation unit through self-cleaning strainer except the air of dust, mechanical admixture.Air after compression, through chilldown system precooling, then enters purification system, through molecular sieve adsorber purification, removes the moisture content, carbon dioxide, acetylene, propylene, propane etc. in air.Air after purification is low temperature air cooled but to condensing temperature by the upper and lower tower backflowed in main heat exchanger, enters Xia Ta and carries out initial gross separation.Lower tower bottom is oxygen-enriched liquid air, and top is highly purified nitrogen and liquid nitrogen.Liquid air, liquid nitrogen throttling enter the further rectifying of upper tower, obtain liquid oxygen (>=99.6%O2), draw as product in condenser/evaporator.Extract argon fraction (8% ~ 12%Ar) in the middle part of upper tower out and remove argon producing system, through crude argon column deoxygenation, pure argon column is denitrogenated, bottom pure argon column, finally obtain smart argon (≤2PPmO2 ,≤3PPmN2) product.Lower top of tower extracts pressure nitrogen out, and supercharging in cyclic nitrogen press, expansion throttling obtains fraction low pressure liquid nitrogen, and most of low-pressure nitrogen enters cyclic nitrogen press.
The traditional sky of LNG cold energy process features is utilized to divide rectifying to be provide cold by choke valve and expander refrigeration machine.Adopt low-temperature circulating nitrogen compressor, first in liquefier, be cooled to about 150K enters nitrogen compressor to circulating nitrogen gas again, and the cascade EDFA of nitrogen compressor also carries out in liquefier, in liquefier, the cold energy of LNG is only utilized at-151 DEG C ~-73 DEG C temperature sections, the cold of high temperature section is by cooling glycol water, make natural gas re-heat to normal temperature, cooled glycol water goes the intercooler of air compressor machine to make cascade EDFA.
In sum, prior art utilizes LNG cold energy to produce the method for the industrial gasses products such as liquid nitrogen, and system equipment is huge, complex structure, and production cost is high, and workflow link is loaded down with trivial details.
Summary of the invention
The object of the invention is the weak point existed for above-mentioned prior art, there is provided a kind of structure simple, production cost is low, LNG cold energy use rate is high, nitrogen compressor pressure rating and heat exchanger pressure rating can be reduced, reduce nitrogen circulation amount, save energy consumption, recycle the system that LNG cold energy carries out liquefaction of nitrogen.
Concrete scheme of the present invention is: a kind of nitrogen gas liquefaction system recycling LNG cold energy, comprises the liquefaction of nitrogen circulatory system and programmable controller PLC control system.Nitrogen circulation liquefaction system comprises the three groups of step cold heat exchangers connected in turn by one-level, secondary, three grades of priorities, it is characterized in that: nitrogen circulation liquefaction system is provided with low-temperature circulating Nitrogen pipe network system and middle pressure natural gas transport pipe network system, at low-temperature circulating Nitrogen pipe network output and the LNG pipe network input of three grades of nitrogen cryogenic liquefying heat exchangers 3, be respectively equipped with LNG choke valve 4 and liquid nitrogen choke valve 5 that programmable controller PLC controls throttling degree; From the nitrogen of top of tower on air separation column after normal temperature compressed machine 6 compresses, in the nitrogen precooled heat exchanger 1 of one-level, carry out heat exchange precooling with the low-pressure low-temperature natural gas from LNG choke valve 4 throttling re-heat, be chilled to-100 DEG C to-115 DEG C in advance; Low temperature nitrogen after precooling carries out heat exchange with the middle LNG of pressure in cold heat exchanger 2 and obtains cold nitrogen in-135 DEG C to-145 DEG C in secondary nitrogen; In cold nitrogen by three grades of nitrogen cryogenic liquefying heat exchangers 3 absorb from LNG through choke valve 4 throttling gasification produce-160 DEG C ultralow temperature cold energy liquefaction, the liquid nitrogen temperature of post liquefaction is down to-155 DEG C to-158 DEG C, most of low pressure liquid nitrogen that liquid nitrogen produces after choke valve 5 throttling is as product introduction liquid nitrogen storage tank, small part low-pressure nitrogen, as circulating nitrogen gas, backflows after re-heat to nitrogen compressor 6 entrance and recompresses in the nitrogen precooled heat exchanger 1 of one-level.
The present invention has following beneficial effect compared to prior art.
Structure is simple.Three groups of step cold heat exchangers that the present invention connects by one-level, secondary, three grades of sequencings, by LNG choke valve, liquid nitrogen throttle valve control throttle degree that programmable controller PLC control system controls, LNG endless-chain is short, solves the problem that prior art each link step is connected difficult, LNG cold energy use rate is low.
Reduce the pressure rating of nitrogen circulation liquefaction system.The present invention adopts nitrogen staged to cool, liquefaction, full liquid space division conventional compared to tradition, significantly reduce the pressure rating of nitrogen compressor and corresponding reduction heat exchanger and pipeline pressure grade, decrease the nitrogen circulation amount of liquid nitrogen throttling with pressure, reduce equipment investment, raising production capacity has saved energy consumption simultaneously.
Liquid nitrogen production capacity improves, and energy consumption reduces.The present invention adopts nitrogen staged to cool, liquefaction, and full liquid space division conventional compared to tradition, decreases the nitrogen circulation amount of liquid nitrogen throttling with pressure, improve liquid nitrogen production capacity and significantly reduce specific yield energy consumption with the time.
The cold mist pollution brought when eliminating the gasification of LNG empty bath formula.The present invention fully absorbs LNG cold energy, alleviates the cold mist pollution brought when LNG air-bathing gasifier load eliminates the gasification of LNG empty bath formula simultaneously.
The integrated low-temperature temperature circulating nitrogen gas pipe network system that the present invention utilizes the liquefaction of nitrogen circulatory system to arrange and the step circulation process form of LNG transmission pipeline network system, make nitrogen complete by once pre-cooled, in be cooled to liquefaction, not only circulating nitrogen gas pressure rating reduces, reduce equipment investment, also improve liquid nitrogen production because reducing cyclic nitrogen tolerance, thus reduce unit liquid output energy consumption.Fluid product energy consumption of the present invention is not higher than 350 kilowatt-hours/ton, and the liquid energy consumption that the full liquid space division system of the routine of technological state of the art is produced relatively is in the world 850 kilowatt-hours/ton, reduces 58.8%.Solve prior art air direct expansion circulation cold flow, outer circulation swell refrigeration flow process, precooling outer circulation swell refrigeration flow process, the two swell refrigeration flow process of outer circulation, outer liquefying refrigerating circulation process, large-scale interior compression air separation plant system are huge, complex structure, the problem that the energy consumption produced in fluid product preparation is higher.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in further detail.
Fig. 1 is the process flow system schematic diagram that a kind of LNG of utilization cold energy provided by the invention carries out nitrogen at room liquefaction.
In figure: cold heat exchanger, 3 three grades of nitrogen cryogenic liquefying heat exchangers, 4LNG choke valve, 5 liquid nitrogen choke valves, 6 nitrogen at room compressors in the nitrogen precooled heat exchanger of 1 one-level, 2 secondary nitrogen, 7 normal-temperature natural-gas compressors.
Detailed description of the invention
Consult Fig. 1.In embodiment described below, the system that recycling LNG cold energy carries out liquefaction of nitrogen comprises cold heat exchanger 2, one group three grades nitrogen cryogenic liquefying heat exchangers 3, LNG choke valve 4, liquid nitrogen choke valve 5, nitrogen at room compressor 6 and a normal-temperature natural-gas compressor 7 in the nitrogen precooled heat exchanger of the one group of one-level connected in turn 1, one group of secondary nitrogen.Nitrogen circulation liquefaction system is provided with low-temperature circulating Nitrogen pipe network system and middle pressure natural gas transport pipe network system, at low-temperature circulating Nitrogen pipe network output and the LNG pipe network input of three grades of nitrogen cryogenic liquefying heat exchangers 3, be respectively equipped with LNG choke valve 4 and liquid nitrogen choke valve 5 that programmable controller PLC controls throttling degree.The high pure nitrogen gone out from top of tower rectifying on air separation column carries out heat exchange reach precooling object as entrance nitrogen at room and 0.1MPa ~ 0.02MPa low pressure, the cryogenic natural gas produced after choke valve 4 throttling with LNG in the nitrogen precooled heat exchanger 1 of one-level after nitrogen frequent temperature compressor 6 is compressed to 2.0MPa ~ 2.5MPa that backflow after re-heat.After precooling, nitrogen temperature scope is-100 DEG C to-115 DEG C.Low temperature nitrogen after precooling in secondary nitrogen in cold heat exchanger 2 with 0.3MPa ~ 0.4MPa in press LNG carry out heat exchange obtain in cold nitrogen, in cold rear nitrogen temperature scope be-135 DEG C to-145 DEG C.In cold nitrogen absorb in three grades of nitrogen cryogenic liquefying heat exchangers 3 LNG gasify after choke valve 4 throttling produce ultralow temperature (-160 DEG C or following) cold and liquefy, liquid nitrogen temperature scope is-155 DEG C to-158 DEG C; High-pressure liquid nitrogen produces-188 DEG C to-196 DEG C low pressure liquid nitrogen and low-pressure nitrogen after liquid nitrogen choke valve 5 throttling, low pressure liquid nitrogen is as the low-temperature receiver of product and air separation column, and low-pressure nitrogen backflows after re-heat to nitrogen compressor 6 entrance as circulating nitrogen gas and recompresses in the nitrogen precooled heat exchanger 1 of one-level.Low pressure natural gas is compressed to middle pressure (0.4MPa) with pressing in after cold heat exchanger 2 in secondary nitrogen together with (0.4MPa) natural gas through normal-temperature natural-gas compressor 7 and enters natural gas medium-pressure pipe network for natural gas user after the nitrogen precooled heat exchanger of one-level 1.LNG controls its throttle degree through choke valve 4 and liquid nitrogen choke valve 5 by PLC.
Claims (7)
1. recycle the nitrogen gas liquefaction system of LNG cold energy for one kind, comprise the liquefaction of nitrogen circulatory system and programmable controller PLC control system, nitrogen circulation liquefaction system comprises by one-level, secondary, three groups of step cold heat exchangers that three grades of priorities connect in turn, it is characterized in that: nitrogen circulation liquefaction system is provided with low-temperature circulating Nitrogen pipe network system and middle pressure natural gas transport pipe network system, from top of tower on air separation column nitrogen through normal temperature compressed machine (6) compression after, heat exchange precooling is carried out with the low-pressure low-temperature natural gas from LNG choke valve (4) throttling re-heat in the nitrogen precooled heat exchanger of one-level (1), be chilled to-100 DEG C to-115 DEG C in advance, low temperature nitrogen after precooling carries out heat exchange with the middle LNG of pressure in cold heat exchanger (2) and obtains cold nitrogen in-135 DEG C to-145 DEG C in secondary nitrogen, in cold nitrogen absorbed the ultralow temperature cold energy liquefaction of-160 DEG C produced through choke valve (4) throttling gasification from LNG by three grades of nitrogen cryogenic liquefying heat exchangers (3), the liquid nitrogen temperature of post liquefaction is down to-155 DEG C to-158 DEG C, most of low pressure liquid nitrogen that liquid nitrogen produces after choke valve (5) throttling is as product introduction liquid nitrogen storage tank, small part low-pressure nitrogen, as circulating nitrogen gas, backflows after re-heat in the nitrogen precooled heat exchanger of one-level (1) to nitrogen compressor (6) entrance and recompresses.
2. the nitrogen gas liquefaction system recycling LNG cold energy as claimed in claim 1, it is characterized in that: the high pure nitrogen gone out from top of tower rectifying on air separation column after re-heat as entrance nitrogen at room, after being compressed to 2.5MPa with the frequent temperature compressor (6) of the nitrogen that backflows, the 0.02MPa low-pressure low-temperature natural gas produced after choke valve (4) throttling with LNG in the nitrogen precooled heat exchanger of one-level (1) carries out heat exchange precooling.
3. the nitrogen gas liquefaction system recycling LNG cold energy as claimed in claim 1, it is characterized in that: high-pressure liquid nitrogen produces-188 DEG C to-196 DEG C low pressure liquid nitrogen and low-pressure nitrogen after liquid nitrogen choke valve (5) throttling, low pressure liquid nitrogen is as the low-temperature receiver of product and air separation column.
4. the as claimed in claim 1 nitrogen gas liquefaction system recycling LNG cold energy, is characterized in that: low-pressure nitrogen backflows to nitrogen compressor (6) entrance as circulating nitrogen gas and recompresses after re-heat in the nitrogen precooled heat exchanger of one-level (1).
5. the nitrogen gas liquefaction system recycling LNG cold energy as claimed in claim 1, it is characterized in that: low pressure natural gas is after the nitrogen precooled heat exchanger of one-level (1), be compressed in 0.4MPa through normal-temperature natural-gas compressor (7) and press, enter natural gas medium-pressure pipe network for natural gas user with pressing in the 0.4MPa after cold heat exchanger (2) in secondary nitrogen together with natural gas.
6. the nitrogen gas liquefaction system recycling LNG cold energy as claimed in claim 1, is characterized in that: LNG controls its throttle degree through choke valve (4) and liquid nitrogen choke valve (5) by PLC.
7. the nitrogen gas liquefaction system recycling LNG cold energy as claimed in claim 1, it is characterized in that: at low-temperature circulating Nitrogen pipe network output and the LNG pipe network input of three grades of nitrogen cryogenic liquefying heat exchangers (3), be respectively equipped with LNG choke valve (4) and liquid nitrogen choke valve (5) that programmable controller PLC controls throttling degree.
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| CN106885448B (en) * | 2015-12-16 | 2019-05-07 | 中国石油天然气集团公司 | Utilize the air-separating technology of high-pressure liquefaction natural gas cold energy |
| CN105605419B (en) * | 2015-12-31 | 2018-08-07 | 杰瑞石油天然气工程有限公司 | Empty nitrogen station cold energy comprehensive reutilization system and its recoverying and utilizing method |
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| CN110645770A (en) * | 2019-09-22 | 2020-01-03 | 浙江智海化工设备工程有限公司 | Liquid argon cold energy recovery method |
| CN110779277B (en) * | 2019-11-25 | 2023-05-23 | 杭氧集团股份有限公司 | Air separation energy-saving device for producing liquid nitrogen by utilizing LNG cold energy and mixed refrigeration working medium circulation |
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| CN111578139B (en) * | 2020-05-22 | 2023-04-07 | 哈尔滨锅炉厂有限责任公司 | LNG cold energy and temperature difference double-loop and gas three-layer coupling power generation method |
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| CN114748968B (en) * | 2022-06-10 | 2022-09-23 | 常州大恒环保科技有限公司 | Energy storage type organic tail gas recovery method and device utilizing liquid nitrogen cold energy |
| CN115420062B (en) * | 2022-08-26 | 2024-03-22 | 中国舰船研究设计中心 | Marine nitrogen liquefaction system and method |
| CN116987536B (en) * | 2023-06-15 | 2024-03-08 | 英德市西洲气体有限公司 | Argon removal process for methane tower |
| CN117937775B (en) * | 2024-03-25 | 2024-06-18 | 浙江浙能技术研究院有限公司 | Energy storage power generation system operated in combination with LNG receiving and transferring station |
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